US7857964B2 - Method of refining heavy oil and refining apparatus - Google Patents

Method of refining heavy oil and refining apparatus Download PDF

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US7857964B2
US7857964B2 US10/468,508 US46850803A US7857964B2 US 7857964 B2 US7857964 B2 US 7857964B2 US 46850803 A US46850803 A US 46850803A US 7857964 B2 US7857964 B2 US 7857964B2
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oil
concentration
refining
poly
extraction
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US20040084351A1 (en
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Yoshinori Mashiko
Akira Sugimoto
Tsuyoshi Okada
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JGC Corp
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/0463—The hydrotreatment being a hydrorefining
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/003—Solvent de-asphalting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/14—Hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/30—Controlling or regulating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0409—Extraction of unsaturated hydrocarbons
    • C10G67/0418—The hydrotreatment being a hydrorefining
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0409—Extraction of unsaturated hydrocarbons
    • C10G67/0436—The hydrotreatment being an aromatic saturation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/049—The hydrotreatment being a hydrocracking
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S208/00—Mineral oils: processes and products
    • Y10S208/01—Automatic control

Definitions

  • the present invention relates to method and facility for refining heavy oil wherein the conditions of the hydrogenation process that become severe due to impurities in the crude oil source can be improved, and thereby the hydrogenation process can be carried out under mild conditions.
  • a first aspect of the present invention is a refining method for refining heavy oil and obtaining refined oil, and this method comprises a solvent extraction process in which an extracted oil is obtained by a solvent extraction process, and a hydrorefining process in which the refined oil is obtained by hydrogenating the obtained extracted oil in the presence of hydrogen and a catalyst; and further comprises the steps of detecting the specific component concentrations in the extracted oil obtained by the solvent extraction process and controlling the extraction conditions depending on these detected values.
  • the extracted oil obtained by the solvent extraction process in addition to hydrocarbons, there is residual sulfur, nitrogen, oxygen, nickel, vanadium, and the like. In order to eliminate these residual components to obtain various types of oil products and intermediate oil products, the extracted oil further undergoes a hydrogenation process.
  • SL-VR denotes Sumatra Light-Vacuum Residue
  • DURI-VR denotes Duri-Vacuum Residue
  • MR-VR denotes Murban-Vacuum Residue
  • AL-VR denotes Arabian Light-Vacuum Residue
  • ALH-VR denotes Arabian Light Vacuum Residue Arabian Heavy Vacuum Residue (60, 40 mixed).
  • asphaltene is heptane insoluble (C7-insoluble, below abbreviated “C7Insol”).
  • FIG. 3 shows the relationship between the type of the extraction solvent (the carbon number of the solvent) and the yield (extraction rate) of the deasphalted oil in the case that the solvent extraction process was carried out using the vacuum residue of Arabian Light as a feed oil.
  • the solvents denoted by Cn are linear saturated hydrocarbons (alkanes) having n carbon atoms.
  • the solvent extraction process is carried out for each of the vacuum residues of the five types of feed oil described above, and the residual rates of each of the impurities in the deasphalted oil (extracted oil) for the yield (extraction rate) of the deasphalted oil were found.
  • the average characteristics of this feed oil is shown in FIG. 4 .
  • S denotes the sulfur that is an impurity
  • N similarly is nitrogen
  • C denotes Conradson carbon residue
  • Ni denotes Nickel
  • V denotes vanadium.
  • the diagonal line in FIG. 4 denotes that no selection of any kind was made for the extraction rate, and is a line signifying that when the extraction rate is high, the impurities described above were uniformly extracted depending on the extraction rate.
  • the extraction rate by the solvent extraction process changes depending on the type of solvent. However, in addition to the type of solvent, it can also be changed due to such operating factors (control factors) as the extraction temperature and the rate of flow of the solvent.
  • control factors for example, as shown in FIG. 5 , by changing the extraction temperature (the process temperature of the extraction process), the yield of the deasphalted oil (extracted oil) can be changed. That is, according to FIG. 5 , it can be understood that the extraction rate can be lowered by raising the extraction temperature.
  • the feed oil was SL-VR
  • the pressure was 35 kg/cm 2 G
  • the solvent was a butane mixture.
  • the weight ratio of the solvent/to the supplied oil was 6.
  • the yield of deasphalted oil can also be changed by changing the rate of flow of solvent (the weight ratio of the solvent/supplied oil). That is, according to FIG. 6 , it can be understood that by raising the rate of flow of solvent, the extraction rate can be lowered.
  • the feed oil was DURI-VR
  • the pressure was 35 kg/cm 2 G
  • the solvent was a butane mixture.
  • the extraction temperature was 100° C.
  • reaction conditions (process conditions) of hydrogenation processes such as desulfurizing, demetalizing, denitrifying, and hydrocracking are strongly related to the extraction rate, and as shown in FIG. 7 , where the extraction rate is high, the reaction conditions become severe.
  • FIG. 7 shows the relationship between the yield (extraction rate) of the deasphalted oil (extracted oil) and the conversion rate due to hydrocracking.
  • the hydrocracking activity rapidly decreases.
  • the relationship between this extraction rate and the conversion rate is the result of combining carrying out the solvent extraction process by using the vacuum residue of Arabian light as a feed oil and carrying out hydrogenation process on the obtained deasphalted oil (extracted oil).
  • the fraction that cannot be fractionally distilled is separated into the following fractions by column chromatographic analysis using a solvent and an absorbent.
  • the solvent is eliminated from the recovered fractions, the weight of each of the fi-actions is measured, and the content is calculated.
  • each has an extremely high boiling point, and in particular, the PP (poly-aromatics component) includes components that do not distill out even at 1100° C. In addition, the residue has a boiling point that is too high to measure.
  • PP poly-aromatics component
  • FIG. 9 shows the result of studying how the amount of each component included in the feed oil that migrates to the extracted oil changes depending on the extraction rate. According to FIG. 9 , it can be understood that the SA, MA, DA, TA and the like that are above the diagonal line (not illustrated) are extracted excessively as this extraction rate, while in contrast, almost no PP and Residue (C7Insol), which are below the diagonal line (not illustrated), are extracted at a very low extraction rate.
  • FIG. 7 shows that the reaction in the hydrogenation process (hydrocracking) becomes rapidly lower when the extraction rate of the deasphalted oil (extracted oil) exceeds 60 to 85%. From the results shown in FIG. 9 , we consider this to be due to the concentration of the residue (C7Insol) in the extracted oil (deasphalted oil) that will serve as the processed oil heavily influencing the reactive operation of the hydrogenation process.
  • results shown in FIG. 9 are shown in FIG. 10 as the relationship between the extraction rate and the action of each component shown using the feed oil as the reference.
  • the yield of each of the components for each of the extraction rates is the value shown by the interval between each of the curves (where SA is the value shown by the interval between the curve and the X-axis, and C7Insol is the value shown by the interval between the diagonal line and the curve).
  • Feed oils were prepared having amounts (wt %) of each impurity shown below:
  • these feed oils were respectively subject to the solvent extraction process in a range of 30 wt % to 90 wt % at 5 wt % intervals.
  • the amount of each of the impurities was measured by the column chromatographic analysis method described above.
  • the refining method for heavy oil of the present invention is characterized in that the predetermined component concentration in the extracted oil obtained by the solvent extraction process is detected, and at the same time the extraction conditions are controlled according to these detected values.
  • the predetermined component described above is, for example, C7Insol, and this is set equal to or less than a particular concentration, that is, the amount of C7Insol is set to an amount just before the point that the reaction of the hydrogenation process decreases rapidly, by subjecting the extracted oil obtained in this manner to a hydrogenation process, the reaction can be manipulated under comparatively mild conditions. Therefore, the drawbacks that the maintenance of the hydrogenation process apparatus consumes much time, that the cost is high, and that the service life of the apparatus itself is short, can be improved.
  • the value of the C7Insol to PP is substantially constant (in the example of Table 1, 0.140 to 0.152, where these values change depending on the type of feed oil). Therefore, within this range, it is understood that the value of the PP can be used as the index instead of the value of C7Insol.
  • one of the characteristics of the refining method of heavy oil according to the present invention is setting predetermined values for the concentration of the heptane insoluble components in the fraction of the extracted oil obtained by the solvent extraction process that cannot be fractionally distilled, that is, the concentration of the poly-aromatic component in the fraction that cannot be fractionally distilled, or in other words, the concentration of the heptane insoluble components assigned based on the PP.
  • Poly-aromatic components comprise the poly-aromatics and polar compounds described above, and the concentration thereof can be measured continuously by analyzer such as a Near Infrared Spectroscopic Analyzer or a Nuclear Magnetic Resonance Analyzer.
  • the correlation between the detection signal obtained by these analyzer and the concentration of the PP can be clarified in advance experimentally, and furthermore, as shown in Table 1, the correlation between the concentration of the PP and the concentration of the C7Insol can be clarified in advance.
  • the concentration of the C7Insol can be known from the concentration of the PP obtained by the analyzers.
  • a calibration curve can be established by finding the correlation between the concentration of the C7Insol and the concentration of the poly-aromatics during the extraction and refining by using extraction conditions for the feed oil that is the object of refining and the extraction solvents.
  • the poly-aromatic concentration information corresponding to this normal value is input into the control device of the refining facility, and thereby the concentration of this C7Insol can be indirectly controlled.
  • the poly-aromatic concentration corresponding to the C7Insol determined according to the specifications of the target refined oil serve as the normal value, and in the case that the detected value in the extracted oil is large with respect to this normal value, the extraction conditions are controlled so that the extraction rate is lowered, and in the case that the detected value in the extracted oil is small with respect to the normal value, the extraction rate in the extraction process step is controlled so as to increase.
  • This normal value can have a predetermined range, and in this case, the conditions can be controlled with respect to a maximum or minimum value thereof.
  • the operating conditions (process conditions) in the hydrogenation process which is one of the later stages in this solvent extraction process, do not become severe, and can be made comparatively mild conditions.
  • the refining method for heavy oil according to the present invention is characterized in that, because it was discovered that the C7Insol in the extracted oil is correlated with the poly-aromatic concentration, the extraction process can be indirectly controlled so that the C7Insol in the refined oil remains equal to or less than a predetermined concentration by using the poly-aromatic concentration in the extracted oil as an index. Furthermore, the hydrorefining process can be controlled so that the C7Insol in the hydrorefined oil obtained in the hydrorefining process subsequent to the extraction process finally becomes equal to or less than a predetermined concentration.
  • the refining facility for heavy oil is characterized in providing a detecting device that detects the concentration of the poly-aromatic component in the extracted oil obtained by the solvent extraction process and a control device that controls the process conditions of the solvent extraction process apparatus depending on the values provided by the detecting device, and furthermore, a device that controls the refining conditions of the hydrorefining unit provided in the later stage of the solvent extraction unit is provided.
  • the desired degree of refining in other words, the amount of C7Insol included
  • the concentration of poly-aromatics as an index
  • the operating conditions of the hydrorefining provided in the later stages of the solvent extraction can be operated under relatively mild conditions.
  • facility expenses such as the operating cost, the maintenance cost, and the like can be decreased. Therefore, grades of oil products can be and economically easily manufactured according to their economic object.
  • FIG. 1 is a drawing showing the schematic structure of the embodiment of the refining facility for heavy oil according to the present invention.
  • FIG. 2 is a drawing showing a schematic structure of the solvent extraction process apparatus in the refining facility for heavy oil shown in FIG. 1 .
  • FIG. 3 is a graph showing the relationship between the type of extraction solvent (the carbon number of the solvent) and the deasphalted oil extraction rate.
  • FIG. 4 is a graph showing the residual rate of each of the impurities in the deasphalted oil with respect to the extraction rate of the deasphalted oil.
  • FIG. 5 is a graph showing the relationship between extraction temperature and the extraction rate of the deasphalted oil.
  • FIG. 6 is a graph showing the relationship between the flow rate of the solvent and the extraction rate of the deasphalted oil.
  • FIG. 7 is a graph showing the relationship between the extraction rate of the deasphalted oil and the transfer rate due to hydrocracking.
  • FIG. 8 is a graph showing the distillation properties of the residue.
  • FIG. 9 is a graph showing the relationship between the extraction rate of the deasphalted oil.
  • FIG. 10 is a graph showing the relationship between the extraction rate of the deasphalted oil and the concentration of each of the residues in the deasphalted oil.
  • FIG. 1 is a drawing showing an embodiment of the refining facility for heavy oil according to the present invention, where reference numeral 1 in the drawing denotes the refining facility for heavy oil.
  • This refining facility 1 is a facility that refines grades of oil from a feed oil according to their object, and provides a solvent extraction process unit 2 and a hydrogenation process unit 3 .
  • An analyzer 4 that detects the concentration of the poly-aromatics in the obtained extracted oil is provided at the later stage of the solvent extraction process unit 2 .
  • the solvent extraction process unit 2 is a unit that obtains an extracted oil by carrying out the solvent extraction process on the feed oil, and as shown in FIG. 2 , provides an extraction column 5 . In this extraction column 5 , the solvent extraction process is carried out.
  • the solvent extraction process unit 2 provides a process temperature control apparatus 6 that controls the temperature of the extraction process that is carried out in the extraction column 5 and a solvent flow rate control apparatus 7 that controls the flow rate of the solvent that flows into the extraction column 5 .
  • a control program set in advance based on the concentration of the poly-aromatics (PP) in the extracted oil obtained by the analyzer 4 , which will be explained below.
  • the hydrogenation process unit 3 is a unit that carries out hydrogenation process on the extracted oil obtained by the solvent extraction process unit 2 in the presence of hydrogen and a catalyst to obtain a hydrorefined oil, and generates various types of oil products or intermediary oil products such as the raw material for fluid catalytic cracking (FCC), which is the refined oil according to their object.
  • FCC fluid catalytic cracking
  • the concrete processing by the hydrogenation process unit 3 includes all reactions that occur in the presence of hydrogen and a catalyst, and generally comprise a hydrocracking reaction, a hydrodesulfurizing reaction, a hydrodemetalizing reaction, and a hydrodenitrifying reaction.
  • hydrocracking reaction hydrocarbons are cracked under high temperature and high pressure in a hydrogen atmosphere, and a low atomic weight refined oil is obtained from the processed oil (extracted oil).
  • hydrodesulfurizing reaction sulfur compounds in the hydrocarbons are reacted with hydrogen under high temperature and high pressure in a hydrogen atmosphere to form hydrogen sulfide.
  • the hydrogen sulfide is separated, and a refined oil having a lower sulfur concentration than the processed oil (extracted oil) is obtained.
  • the metal compounds in the carbohydrates are hydrogenated under high temperature and high pressure in a hydrogen atmosphere to form elemental metals which are then deposited on the catalyst. Thereby, a refined oil having a metal concentration that is lower than the processed oil (extracted oil) is obtained.
  • the nitrogen compounds in the hydrocarbons are reacted with hydrogen under a high temperature and high pressure in a hydrogen atmosphere to obtain ammonia.
  • the ammonia is separated to obtain a refined oil having a nitrogen concentration that is lower than the processed oil (extracted oil).
  • a factors that control the reaction rate comprise the ratio of supplied hydrogen to feed oil, the ratio of the volumetric flow rate (LHSV: liquid hourly space velocity) to the catalyst, the reaction temperature, the catalyst type, and the like, and these respectively differ depending on the type of hydrogenation process that is the general object.
  • LHSV volumetric flow rate
  • the reaction pressure, size of the reaction vessel, and the like are fixed based on the apparatus design, and therefore among the control factors described above, the preferable objects of control are the hydrogen to oil ratio, the reaction temperature, and the flow rate of the extracted oil.
  • the hydrogenation process unit 3 described above provides a reaction temperature control apparatus 8 that controls the reaction temperature in this hydrogenation process unit 3 and a extracted oil flow rate control apparatus that controls the flow rate of the extracted oil that flows into this hydrogenation process unit 3 .
  • a reaction temperature control apparatus 8 that controls the reaction temperature in this hydrogenation process unit 3
  • a extracted oil flow rate control apparatus that controls the flow rate of the extracted oil that flows into this hydrogenation process unit 3 .
  • These are structured so as to control the reaction temperature or extracted oil flow rate so as to form optimal hydrogenation conditions by a control program that is set in advance based on the concentration of the poly-aromatics (PP) in the extracted oil obtained on the analyzer 4 explained next.
  • PP poly-aromatics
  • the NIR analyzer or the NMR analyzer described above is preferably used as an analyzer 4 .
  • Each of the control apparatuses described above, specifically, the process temperature control apparatus 6 and the solvent flow rate control apparatus 7 in the solvent extraction process unit 2 and the reaction temperature control apparatus 8 and the extraction oil flow rate control apparatus 9 in the hydrogenation process unit 3 are connected to this analyzer 4 .
  • this analyzer 4 measures the total amount of fraction that cannot be fractionally distilled from a given amount of extracted oil and the amount of PP (poly-aromatics) therein are measured, and by mathematical processing of this result, the concentration of the poly-aromatics (PP) in the extracted oil, that is, the concentration of poly-aromatics (PP) in the fraction of the extracted oil that cannot be fractionally distilled, is detected.
  • the solvent extraction process of the feed oil is carried out in the solvent extraction process unit 2 .
  • this solvent extraction process unit 2 first, as shown in FIG. 2 , the feed oil is sent to the feed oil storage tank 10 and stored there, while the solvent is sent to the solvent storage tank 11 and stored there.
  • the feed oil and the solvent are supplied to the extraction column 5 , which is controlled so as to maintain a predetermined pressure and temperature. Here they are mixed and the extraction process is carried out.
  • the obtained extracted oil is separated from the solvent by the extraction oil/solvent separating device 12 .
  • the solvent remaining in the extracted oil is removed by the extracted oil separating column 13 , and subsequently sent to the extracted oil storage tank 14 to be stored therein.
  • the solvent is separated from the residue obtained from the extraction column 5 by the residue/solvent separating device 15 to be finally stored in the residue storage tank 16 .
  • the concentration of the poly-aromatics (PP) is continuously detected by the analyzer 4 .
  • the obtained results are converted to a detection signal and respectively sent (as feedback) to the process temperature control apparatus 6 and the solvent flow rate control apparatus 7 of the solvent extraction process unit 2 as well as the reaction temperature control apparatus 8 and the extraction oil flow rate control apparatus 9 in the hydrogenation process unit 3 .
  • the analyzer 4 continuously carried out detection to the extent that this does not hinder the operation of the extraction unit, for example, at 5 minute intervals.
  • the extraction temperature is raised and the extraction rate is lowered by the process temperature control apparatus 6 when, for example, the value of the PP is higher than the 40.2 wt % (refer to Table 1) that corresponds to the 6.1 wt %, which is the reference concentration of the C7Insol, and thereby the value of the PP (that is, the concentration of the C7Insol) is lowered.
  • the flow rate of the solvent can be raised and the extraction rate lowered by the solvent flow rate control apparatus 7 , and thereby the value of the PP (that is, the concentration of the C7Insol) lowered.
  • both controls can be carried out simultaneously, or only one of them can be carried out. The efficiency is investigated experimentally in advance from the point of view of cost and production efficiency, and these controls are programmed in advance so as to establish optimal conditions.
  • the hydrogenation process can be carried out under operating conditions that are optimal for the properties of this extracted oil.
  • the reaction conditions in the hydrogenation process unit 3 are not severe, and the process can be carried out under mild conditions. In contrast, these conditions are not necessarily the best reaction conditions corresponding to the concentration of the PP (that is, the concentration of the C7Insol that characterizes it) if the process is simply carried out under constant conditions.
  • the hydrogenation process unit 3 based on the data detected and sent by the analyzer 4 , that is the amount (concentration) of the PP for the extracted oil that becomes the processed oil stored in the extracted oil storage tank 14 , either one or both of the reaction temperature control apparatus 8 and the extracted oil flow rate control apparatus 9 are controlled, and thereby the process can be carried out under mild conditions that are mild and that sufficiently satisfy the properties of the object oil product (or intermediate oil product).
  • these controls like the case of the solvent extraction process unit 2 described above, the efficiency is investigated in advance experimentally from the point of view of cost and production efficiency, and these controls are programmed in advance so as to establish optimal conditions.
  • the amount (concentration) of the PP of the extracted oil (processed oil) stored in the extracted oil storage tank 14 can be known from the data accumulated by the analyzer 4 described above, and thereby because the concentration of the C7Insol can also be known, for example, by appropriately selecting hydrogenation process unit 3 that differ in type or size, not only the reaction temperature and the extracted oil flow rate described above, but also the reaction pressure and the catalyst type can be suitably selected, and thereby further optimization of the hydrogenation process can be implemented.
  • the feed oil 1 below undergoes the solvent extraction process, and the extracted oil is manufactured.
  • the reaction conditions and reaction rates of the later stages of the hydrogenation process must be taken into account, and the extraction process is controlled such that the concentration of the heptane insoluble (C7Insol) in the fraction of the obtained extracted oil that cannot be fractionally distilled is equal to or less than 5.5 wt %, and the concentration of the poly-aromatic (PP) in the fraction of the extracted oil that cannot be fractionally distilled is equal to or less than 38.5 wt %.
  • Feed oil 1 Feed oil 2 Specific gravity (15/4° C.) 1.032 0.952 Viscosity at 210 F. (cSt) 4327 80 Sulfur concentration (wt %) 4.91 0.19 Ni (ppm) 35 29 V (ppm) 143 0 Asphaltene (wt %) 11.7 0.5 Saturated component (wt %) 4.4 38.5 Mono-aromatics (wt %) 9.9 29.7 Di-aromatics (wt %) 11.3 17.3 Tri-aromatics (wt %) 21.3 8.5 Poly-aromatics (wt %) 40.6 5.3 Solvent insoluble component (wt %) 12.6 0.7
  • the process conditions (operating conditions) of the extraction process apparatus and the properties of the obtained extracted oil are as follows:
  • Extraction results Process Feed oil Feed oil 1 conditions Solvent type pentane Solvent/feed oil mass ratio 2.0 Extraction temperature (° C.) 150 Extraction pressure (kg/cm 2 G) 20 Insoluble component concentration set value 5.5 (wt %) PP value corresponding to insoluble 38.5 component control (wt %) Properties Extracted oil yield (wt %) 79.9 Specific gravity (15/4° C.) 1.002 Viscosity at 210 F. (cSt) 557 Sulfur concentration (wt %) 4.06 Ni (ppm) 8.3 V (ppm) 48.1 Measured insolvent component concentration 5.2 (wt %)
  • the measured insoluble component concentration (heptane insoluble component concentration) becomes 5.2 wt %, and can be produced at the target concentration (equal to or less than 5.5 wt %) of the heptane insoluble component (C7Insol).
  • the object feedstock for the fluidized catalytic cracking can be manufactured by processes at mild reaction conditions that do not place a great load on the hydrogenation process unit.
  • the refining method for heavy oil of the present invention is a method that provides a solvent extraction process that obtains an extracted oil by the solvent extraction process and a hydrorefining process that obtains a hydrorefined oil by subjecting the obtained extracted oil to hydrogenation process in the presence of hydrogen and a catalyst, and detects the concentration of a specified component in the extracted oil obtained in this solvent extraction process, and at the same time, controls the extraction conditions according to these detected values, and thus the hydrorefining process in the stage after the solvent extraction process can be carried out under sufficiently mild conditions, not under severe conditions.
  • the concentration of the heptane insoluble component in the fraction of the extracted oil obtained in the solvent extraction process that cannot be fractionally distilled is defined by the concentration of the poly-aromatics in the fraction that cannot be fractionally distilled, continuous measurement thereof becomes possible, and therefore the process conditions of the hydrogenation process can be rapidly changed based on the measured results, and thereby carrying out the hydrogenation process at conditions that are more severe than necessary can be prevented.
  • the refining facility for heavy oil of the present invention provides a solvent extraction process unit that obtains an extracted oil by the solvent extraction process and a hydrorefining process unit that subjects the obtained extracted oil to hydrogenation process in the presence of hydrogen and a catalyst and obtains a hydrorefined oil
  • the solvent extraction process unit provides a detecting device that detects the concentration of the predetermined component in the extracted oil obtained by the solvent extraction process and a control device that controls the process conditions of the solvent extraction process according to the values obtained by the detecting device, and therefore the residue (heptane insoluble component) in the extracted oil can be defined by detecting, for example, the concentration of the poly-aromatics, and there by not only can the hydrogenation process be carried out under comparatively mild conditions, but of course, various types of oil products and intermediate oil products according to their object can be flexibly produced.

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